CN101778659B - Process for recovering products from fermentation - Google Patents
Process for recovering products from fermentation Download PDFInfo
- Publication number
- CN101778659B CN101778659B CN2008801009078A CN200880100907A CN101778659B CN 101778659 B CN101778659 B CN 101778659B CN 2008801009078 A CN2008801009078 A CN 2008801009078A CN 200880100907 A CN200880100907 A CN 200880100907A CN 101778659 B CN101778659 B CN 101778659B
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- fluid
- temperature
- extraction chamber
- solute
- liquid
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D11/00—Solvent extraction
- B01D11/04—Solvent extraction of solutions which are liquid
- B01D11/0426—Counter-current multistage extraction towers in a vertical or sloping position
- B01D11/0442—Mixers with gas-agitation
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Extraction Or Liquid Replacement (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
The present invention provides a process and an apparatus for transferring a solute from a first fluid to a second fluid immiscible in each other.
Description
Technical field
In the field of substance transfer (mass transfer) operation of the present invention in multiphase system.
Background technology
In the heterogeneous chemical reaction that relates to difficult miscible all liquid reactants, the dispersion of a kind of liquid in all liquid is converted to the fine drop that increases surface area, to improve reaction rate.In order to achieve this end, use physics to disperse usually.Yet, energy that this technological requirement is huge and fund cost.
In a plurality of fields, relate to heterogeneous chemical reaction, said field such as chemical reaction, solvent extraction and from gas stream, isolate ultrafine dust through liquid drop.
The downstream of microorganism fermentation process and further illustrate such problem by reference.Various technologies or any other industrial technology for using from the actual recovered of the useful products that ferments are called downstream.(Downstream Processing, cost DSP) be usually greater than 50% of manufacturing cost, and the product loss is all arranged in each step of DSP for downstream.In addition, product perhaps is present in the unit, perhaps is present in the medium, perhaps in both.
Liquid-liquid extraction is widely used all technology a kind of who is used for reclaiming tunning.In liquid-liquid extraction technology, a kind of (being generally matrix) of liquid filled whole extraction tower by continuous phase, and flows along a direction.Second liquid (being generally solvent) is the fine dispersion phase, and flows along rightabout.Another is mutually required than high surface area in order to obtain material (mass) transferred to from a phase effectively, need meticulous dispersion, and this is a kind of challenge in today.The unique applicable craft that increases the surface area of decentralized photo is that physics disperses, particularly through atomizing.Atomizing relates to the fund cost of expensive atomizer, and external pressure increases the operating cost of technology, makes the technology power consumption serious and cost is high thus.
In general liquid-liquid extraction; In order to produce than high surface area, solvent will be atomized the droplet with the generation solvent, and in order to atomize through atomizer; Need more multipotency, this is infeasible in industry for the product of big volume, low value.
The applicant has paid the surface area of one of the liquid drop of making great efforts to increase dispersing liquid, in the hope of improving the energy efficiency of liquid-liquid extraction technology.The preliminary experiment of being carried out shows, through by means of the steam and the dispersing ultrafine liquid drop that condense in the system, applicant's method can be used for ultrafine dust from gas phase separation effectively, and does not relate to significant amount of energy.
Goal of the invention
Main purpose of the present invention is to increase the surface area of the liquid drop of dispersing liquid phase, to improve the substance transfer operation in multiphase system.Another object of the present invention is, a kind of technology and equipment that is used for solute is transferred to from first fluid second fluid is provided.
Description of drawings
Fig. 1 illustrates the equipment that is used for the butyric acid extraction according to of the present invention.
Fig. 2 illustrates the equipment that is used for alcoholic extract according to of the present invention.
The specific embodiment
Correspondingly; The present invention provides a kind of technology of solute being transferred to second fluid from first fluid; This first fluid and second fluid are difficult each other miscible, and said technology comprises second fluid under gaseous state is incorporated into the step in first liquid that wherein first fluid remains on than under the low temperature of the adiabatic condensation temperature of second fluid; Thereby condensing of first fluid forms ultra-fine fluid fine particle, with from the second fluid extraction solute.
Correspondingly, the invention discloses a kind of through dispersing liquid changed to the technology that liquid is eliminated the defective of above narration from steam.
In one aspect of the invention, when first fluid and second fluid contacted with each other, solute dissolved in this two kinds of fluids.
In another aspect of the present invention, solute is the form of liquid, solid or gas.
Aspect another, the first fluid and second contrary are to flows of the present invention.
The present invention also provides a kind of being used for that solute is transferred to the equipment of second fluid from first fluid, and this first fluid and second fluid are difficult each other miscible, and this equipment comprises:
The extraction chamber remains under first temperature, has first import that is used for supplying with first fluid; Said extraction chamber comprises and is used for second fluid is supplied to second import of extraction in the chamber; Said second import is connected on the storage tank, and this storage tank is suitable for storing second fluid that remains under second temperature; Wherein said first temperature is lower than the adiabatic condensation temperature of second fluid, and said second temperature is higher than the adiabatic condensation temperature of second fluid; Flash tank is connected in first outlet that is arranged on the extraction chamber, is used for admitting the solution of second fluid and solute; Wherein flash tank remains under the 3rd temperature, and the 3rd temperature is higher than the adiabatic condensation temperature of second fluid.
In one aspect of the invention, first import and second import are arranged to, and the first fluid and second fluid supply in the extraction chamber to the direction that flows with contrary.
In another aspect of the present invention, the extraction chamber is provided with the chuck that is used for supplying with the water under predetermined temperature.
Aspect another, storage tank is provided with the chuck that is used for supplying with the water under predetermined temperature of the present invention.
Aspect another, flash tank is provided with the chuck that is used for supplying with the water under predetermined temperature of the present invention.
Illustrate the technology that increases surface area through the liquid-liquid extraction during the fermentation technology process of downstream, wherein change to the surface area that liquid state increases the drop of dispersing liquid from initial gaseous state through liquid phase with dispersing liquid.
Of the present invention many convenient aspect in an aspect in; Dispersing liquid is from such as pentane (36.1 ℃), R143a (1; 1; 1,2-HFC-134a (26.3 ℃)), select in the low boiling point solvent of hexane (69.1 ℃), chloroform (61.2 ℃) and so on, thus removing of solvent do not need other energy.Solvent is through raising some temperature or in flash vessel, form its steam thus separating through flash distillation through reducing pressure, and continuously through extraction tower so that technical process is continuous.
In the present invention, solvent gets into extraction tower or chamber with vapor form, and through coalescent solvent steam in extraction tower, forms the droplet with huge surface area.
And the present invention provides a kind of being used for that solute is transferred to the equipment of second fluid from first fluid, and this first fluid and second fluid are difficult each other miscible.First fluid is a solution to be extracted, and second fluid is a fluid of wherein wanting extract solutes.Equipment of the present invention comprises the extraction chamber.Said extraction chamber can be the form of tower.The extraction chamber has first import and second import, is used for supplying with respectively the first fluid and second fluid.In one embodiment of the invention, first import and second import are arranged in the mode of extraction on the chamber and make the first fluid and second fluid advance to the direction that flows with contrary at the extraction chamber.The extraction chamber remains under first temperature, and this first temperature is lower than the adiabatic condensation temperature of second fluid.Storage tank is connected in second import of extraction chamber, and this storage tank is suitable for being used for comprising second liquid.Storage tank remains under second temperature, and this second temperature is higher than the adiabatic condensation temperature of second fluid.In other words, storage tank comprises second fluid that is steam or gas form.Second liquid that is steam or gas form supplies in the extraction chamber through second import.The steam generation that gets into second fluid of extraction chamber is condensed and is formed the ultrafine dust of liquid, and these ultrafine dusts are from the first liquid extraction solute.Since two kinds of fluids, that is the first fluid and second fluid are difficult each other miscible, so they form the layer that is separated in the extraction chamber.First outlet can be provided in the extraction chamber, is used for collecting the solution of second fluid and solute.And second outlet can be provided in the extraction chamber, is used for collecting first fluid.The solution of the solute second fluid of collecting from the extraction chamber supplies to flash tank.Flash tank can be connected in first outlet of extraction chamber.Flash tank remains under the 3rd temperature, and the 3rd temperature is higher than the adiabatic condensation temperature of second fluid.To supply at the solution of the solute in second fluid and make in the flash tank that second fluid is removed, and stay solute thus.Can from flash tank, extract solute then.
Second outlet can be provided on the extraction chamber, is used for collecting first fluid from the extraction chamber.
In one embodiment of the invention, can on the extraction chamber, chuck be provided, can supply with the water under first temperature, be used for the extraction chamber is remained under first temperature through this chuck.Similarly, chuck can be provided on storage tank, can supply with the water under second temperature, be used for storage tank is remained under second temperature through this chuck.Equally, chuck can be provided on flash tank, can supply with the water under the 3rd temperature, so that flash tank is remained under the 3rd temperature through this chuck.
Temperature can be based on the character of fluid and is selected.
Example:
Following example is not in order to limit scope of the present invention in order to as to illustration of the present invention.
Example 1:
The butyric acid of concentration 6% (w/v) is as feeding solution, and the flow of press 210ml/min passes through 1 meter long extraction tower.The tower content remains under 25 ℃ of low temperature conditions.1 liter of pentane is through the spray column of aqueous solution, and the change in concentration of observing already treated liq, their per at that was collected in tower in 10 minutes.Also confirm the concentration of the resultant product in flash tank.Observed result is given in table-1.Carry out sample analysis with gas chromatography.
Table-1
| Time (in minute) | The concentration of butyric acid raffinate stream (%w/v) |
| 60 | 3.1 |
Example 2:
Keep the reactant and similar experiment condition identical with routine 1, the technology of the application of the invention is carried out similar liquid-liquid extraction.As as carrying out in the control experiment (example 1), liquid phase directly being dispersed in the alternative in the tower, under its gaseous state, supply in the tower, and subsequently gas-phase condensation is become liquid, form the ultrafine dust of dispersing liquid thus.Dispersing liquid, that is 1 liter of pentane is obtained from jar, and through in chuck, using 40 ℃ hot water to be vaporized.Steam is through the spray column of aqueous solution, and wherein the tower temperature is 25 ℃, and this is agglomerated to liquid condition with steam.Liquid drop since its higher density advance downwards, and from solution extract solutes.The concentration of the resultant product in flash tank also is determined.The concentration of the resultant product in flash tank also is determined.Observed result is given in table-2.Carry out sample analysis with gas chromatography.Example 1 and 2 is observed after comparing: under the situation of the surface area increase of the liquid drop that disperses liquid phase, extract very effective.Particularly, in control experiment, obtained 50% the rate of recovery, and this effect obtained in 20 minutes at the 60th minute.
Table-2
Example 3:
The ethanol of concentration 8% (w/v) is as the feeding solution in 1 meter long extraction tower.The solvent that uses is 1,1,1, the 2-HFC-134a, and it is introduced in the tower with vapor form, and the tower content remains under 15 ℃ of low temperature conditions.Steam condenses into liquid condition at low temperatures.Liquid drop since its higher density advance downwards, and from solution extract solutes.The concentration of the resultant product in flash tank also is determined.In the observed result that in table-3, provides, in the time of 10 minutes, obtain 50% rate of recovery.
Table-3
Example 4:
When 2% butanols as feeding material and 1,1,1, the 2-HFC-134a is observed identical trend as the dispersion liquid phase time.In 5 minutes, observe 50% rate of recovery.
Table-4
Example 5:
As shown in fig. 1, pentane steam produces in initial solvent storage tank (1).Through making the hot water between 40 ℃ to 60 ℃ produce pentane steam through the chuck that on extraction tower, provides.The pentane steam that in storage tank (1), produces is delivered to the extraction tower (2) from the bottom of extraction tower (1) through solvent inlet pipe (P1).Moisture butyric acid solution is stored in the solution storage tank (3).Moisture butyric acid solution leads to the extraction tower (2) from the top of extraction tower (2) through solution inlet port pipe (P2) by means of gravity continuously.The temperature of the content of tower (2) remains under the low temperature conditions through using the water at 25 ℃.When pentane steam got in the tower, it condensed and forms little drop, this provide be used for substance transfer than high surface area.The phase transformation of microbubble and formation are important signs of the present invention (phenomenon).Pentane extraction butyric acid, and because pentane is lighter than water so it is up, and forms organic layer at the place, top of extraction tower.The organic layer that comprises pentane and butyric acid is removed from extraction tower (2) through pipeline (P3) through using pump (4) continuously.Handling the liquid of (spent) will remove from the bottom through raffinate pipeline (P4), and this raffinate comprises a spot of butyric acid.After this operation continued some times, technical process got into stable state.To deliver to flash tank (5) through extract from the pentane of extraction container (2) collection and the extract of butyric acid through pipeline (P3).Heat energy is that 40 ℃ hot water is supplied to flash tank (5) through the temperature through chuck, pentane steam flash distillation then, and its steam is recycled to extraction tower through stream (P5).In the end of operation, through using the cold water through chuck, steam can be collected and condense in the coagulation tank (6).Pure butyric acid is collected from flash tank (5) through product outlet stream (P6).
As shown in Figure 2, R134a gas is stored under the pressure of 8bar pressure in the storage tank (1) with liquefied form.R134 delivers to extraction tower (2) from storage tank (1) through solvent inlet pipe (P1) from the top.Aqueous alcohol (ethanol/butanols) solution is stored in the storage tank (3), is pumped into extraction tower (2) through solution inlet port pipe (P2) continuously from solution storage tank (3).The temperature of extraction tower (2) keeps at low temperatures through using the water under 15 ℃.When R134a entered into tower (2), it condensed and forms little drop, thus be provided for substance transfer than high surface area.The phase transformation of microbubble and formation are important signs of the present invention.R134a extracts alcohol (ethanol/butanols), and because R134a is heavier than water, so it is descending, and at bottom formation organic layer.The organic layer that comprises R134a and alcohol (ethanol/butanols) is removed from extraction tower (2) through pipeline (P3) through using pump (4) continuously.Having handled alcohol (ethanol/butanols) will remove from the top, and it comprises the very alcohol of low concentration (ethanol/butanols).After this operation continued some times, technical process got into stable state.The extract of R134a and alcohol (ethanol/butanols) is delivered to flash tank (5) through extraction stream (P3).Heat energy is supplied to flash tank (5) through the hot water under 40 ℃ of temperature through chuck, R134a steam flash distillation then, and its steam is recycled to extraction tower (2) through stream (P4).Absolute alcohol is collected from flash tank (5) through product outlet stream (P5).This experiment must be carried out under the pressure of 8bar.
Claims (8)
1. technology of solute being transferred to second fluid from first fluid; This first fluid and second fluid are difficult each other miscible; Said technology comprises second fluid under gaseous state is incorporated into the step in the said first fluid; Under wherein the said first fluid in the extraction chamber remains on than the low temperature of the adiabatic condensation temperature of said second fluid, thereby condensing of said second fluid forms ultra-fine liquid particle, to extract said solute from said first fluid.
2. technology according to claim 1, wherein, when said first fluid and second fluid contacted with each other, said solute dissolved in this two kinds of fluids.
3. technology according to claim 1, wherein, said solute is the form of liquid, solid or gas.
4. technology according to claim 1, wherein, the said first fluid and the second fluid contrary are to flows.
5. one kind is used for solute is transferred to the equipment of second fluid from first fluid, and this first fluid and second fluid are difficult each other miscible, and this equipment comprises:
(a) the extraction chamber comprises first import that is used for supplying with said first fluid; Said extraction chamber comprises and is used for said second fluid is supplied to second import in the said extraction chamber; Said second import is connected on the storage tank, and this storage tank is suitable for storing second fluid that remains under second temperature; Wherein said second temperature is higher than the adiabatic condensation temperature of said second fluid;
(b) be used for supplying with the chuck of the water under first temperature, in order to said extraction chamber is remained under first temperature, wherein said first temperature is lower than the adiabatic condensation temperature of said second fluid;
(c) flash tank is connected to and is located in first on the said extraction chamber outlet, is used for admitting the solution of second fluid and said solute; Wherein said flash tank remains under the 3rd temperature, and the 3rd temperature is higher than the said adiabatic condensation temperature of said second fluid.
6. equipment according to claim 5, wherein, said first import and said second import are arranged so that said first fluid and said second fluid supply in the extraction chamber to the direction that flows with contrary.
7. equipment according to claim 5, wherein, said storage tank is provided with the chuck that is used for supplying with the water under second temperature.
8. equipment according to claim 5, wherein, said flash tank is provided with the chuck that is used for supplying with the water under the 3rd temperature.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| IN2380CH2006 | 2007-06-20 | ||
| IN2380/CHE/2006 | 2007-06-20 | ||
| PCT/IB2008/001613 WO2008155643A1 (en) | 2007-06-20 | 2008-06-19 | Process for recovering products from fermentation |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101778659A CN101778659A (en) | 2010-07-14 |
| CN101778659B true CN101778659B (en) | 2012-11-07 |
Family
ID=40155956
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008801009078A Expired - Fee Related CN101778659B (en) | 2007-06-20 | 2008-06-19 | Process for recovering products from fermentation |
Country Status (10)
| Country | Link |
|---|---|
| US (1) | US8585902B2 (en) |
| EP (1) | EP2167212A4 (en) |
| JP (1) | JP5364700B2 (en) |
| KR (1) | KR101554465B1 (en) |
| CN (1) | CN101778659B (en) |
| AU (1) | AU2008264875B2 (en) |
| BR (1) | BRPI0811756A2 (en) |
| CA (1) | CA2691240A1 (en) |
| WO (1) | WO2008155643A1 (en) |
| ZA (1) | ZA200909203B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10252216B2 (en) | 2014-09-24 | 2019-04-09 | University Of Kentucky Research Foundation | Reduction of amine emissions from an aqueous amine carbon dioxide capture system using charged colloidal gas aphrons |
Citations (5)
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|---|---|---|---|---|
| US3304341A (en) * | 1962-05-07 | 1967-02-14 | Ici Ltd | Processes for separation of olefines |
| NL7210013A (en) * | 1972-07-20 | 1974-01-22 | Liquid liquid extraction column - using vapour phase extraction to remove dissolved material from original heavy solvent | |
| US4518502A (en) * | 1981-11-04 | 1985-05-21 | Maxwell Laboratories, Inc. | Method of extracting organic contaminants from process waters |
| US5250271A (en) * | 1987-07-24 | 1993-10-05 | Minister Of International Trade & Industry | Apparatus to concentrate and purify alcohol |
| CN1498675A (en) * | 2002-11-06 | 2004-05-26 | 尹恩华 | Method and device for producing ultramicron by using supercritical gas saturation solution |
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| US2200390A (en) * | 1937-05-22 | 1940-05-14 | Pittsburgh Plate Glass Co | Processes of extracting and refining glycerides and products resulting therefrom |
| US2200391A (en) * | 1939-01-17 | 1940-05-14 | Pittsburgh Plate Glass Co | Solvent extraction of glyceride oils |
| US2320738A (en) * | 1940-05-13 | 1943-06-01 | Pittsburgh Plate Glass Co | Fractionation of mixtures of fatty oils and free acids derived therefrom |
| US4251231A (en) * | 1979-09-13 | 1981-02-17 | Artisan Industries Inc. | Direct process for the production of gasohol from fermentation mixtures |
| US4877530A (en) * | 1984-04-25 | 1989-10-31 | Cf Systems Corporation | Liquid CO2 /cosolvent extraction |
| JPH0672861B2 (en) * | 1986-08-04 | 1994-09-14 | 日本碍子株式会社 | NOx sensor |
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| US4954260A (en) * | 1989-06-08 | 1990-09-04 | Zvi Ludmer | Countercurrent separation process and apparatus |
| US4962275A (en) * | 1990-02-21 | 1990-10-09 | United States Of America As Represented By The Secretary Of Commerce | Method and apparatus for supercritical fluid extraction solution separation |
| GB9214379D0 (en) * | 1992-07-07 | 1992-08-19 | Health Lab Service Board | Process for culturing cells |
| US5405533A (en) * | 1993-04-07 | 1995-04-11 | General Atomics | Heat transfer via dense gas in a fluid circulation system |
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| FR2846652B1 (en) * | 2002-10-30 | 2006-09-22 | Rhodia Polyamide Intermediates | PROCESS FOR PRODUCING CARBOXYLIC ACIDS |
| EP1585926A4 (en) * | 2002-12-19 | 2007-09-19 | Karges Faulconbridge Inc | System for liquid extraction, and methods |
| JP2006136780A (en) | 2004-11-11 | 2006-06-01 | Sumitomo Chemical Co Ltd | Method for stopping liquid-liquid extraction column |
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2008
- 2008-06-19 KR KR1020107001072A patent/KR101554465B1/en active IP Right Grant
- 2008-06-19 US US12/665,927 patent/US8585902B2/en not_active Expired - Fee Related
- 2008-06-19 BR BRPI0811756-0A2A patent/BRPI0811756A2/en not_active IP Right Cessation
- 2008-06-19 CN CN2008801009078A patent/CN101778659B/en not_active Expired - Fee Related
- 2008-06-19 EP EP08762930A patent/EP2167212A4/en not_active Withdrawn
- 2008-06-19 WO PCT/IB2008/001613 patent/WO2008155643A1/en active Application Filing
- 2008-06-19 CA CA2691240A patent/CA2691240A1/en not_active Abandoned
- 2008-06-19 JP JP2010512803A patent/JP5364700B2/en not_active Expired - Fee Related
- 2008-06-19 AU AU2008264875A patent/AU2008264875B2/en not_active Ceased
-
2009
- 2009-12-23 ZA ZA200909203A patent/ZA200909203B/en unknown
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| US3304341A (en) * | 1962-05-07 | 1967-02-14 | Ici Ltd | Processes for separation of olefines |
| NL7210013A (en) * | 1972-07-20 | 1974-01-22 | Liquid liquid extraction column - using vapour phase extraction to remove dissolved material from original heavy solvent | |
| US4518502A (en) * | 1981-11-04 | 1985-05-21 | Maxwell Laboratories, Inc. | Method of extracting organic contaminants from process waters |
| US5250271A (en) * | 1987-07-24 | 1993-10-05 | Minister Of International Trade & Industry | Apparatus to concentrate and purify alcohol |
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Also Published As
| Publication number | Publication date |
|---|---|
| BRPI0811756A2 (en) | 2014-11-11 |
| AU2008264875B2 (en) | 2012-12-13 |
| JP2010530747A (en) | 2010-09-16 |
| JP5364700B2 (en) | 2013-12-11 |
| CN101778659A (en) | 2010-07-14 |
| WO2008155643A1 (en) | 2008-12-24 |
| ZA200909203B (en) | 2010-08-25 |
| CA2691240A1 (en) | 2008-12-24 |
| US20100243566A1 (en) | 2010-09-30 |
| KR20100051050A (en) | 2010-05-14 |
| EP2167212A1 (en) | 2010-03-31 |
| EP2167212A4 (en) | 2011-05-18 |
| AU2008264875A1 (en) | 2008-12-24 |
| KR101554465B1 (en) | 2015-09-21 |
| US8585902B2 (en) | 2013-11-19 |
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